EP1656455B1 - Procédé de purification des polypeptides recombinants - Google Patents

Procédé de purification des polypeptides recombinants Download PDF

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Publication number
EP1656455B1
EP1656455B1 EP04764055A EP04764055A EP1656455B1 EP 1656455 B1 EP1656455 B1 EP 1656455B1 EP 04764055 A EP04764055 A EP 04764055A EP 04764055 A EP04764055 A EP 04764055A EP 1656455 B1 EP1656455 B1 EP 1656455B1
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Prior art keywords
polypeptide
interest
process according
fermentation
interferon alpha
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EP1656455A2 (fr
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Günter STEMPFER
Peter Alliger
Norbert Palma
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Sandoz AG
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Sandoz AG
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K14/00—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
    • C07K14/435—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans
    • C07K14/52—Cytokines; Lymphokines; Interferons
    • C07K14/555—Interferons [IFN]
    • C07K14/56—IFN-alpha
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P21/00—Preparation of peptides or proteins
    • C12P21/02—Preparation of peptides or proteins having a known sequence of two or more amino acids, e.g. glutathione

Definitions

  • This invention is concerned with a method for preparation of a recombinant polypeptide of interest, which polypeptide upon expression has been secreted into the periplasm of a transformed host cell.
  • this invention is concerned with methods of preparing and purifying a recombinant human interferon alpha 2.
  • Polypeptides or proteins, like interferons of the group of interferon alpha 2, may be produced by recombinant DNA technology using bacterial cells (e.g. Escherichia coli) as hosts.
  • bacterial cells e.g. Escherichia coli
  • bacterial cells may be transformed with plasmid DNA encoding said polypeptide.
  • the bacteria are thereby enabled to express quantities of the polypeptide in either the cytoplasm or the periplasm. As the bacteria can be grown in large amounts using large-scale fermentation processes, it is possible to produce large quantities of the polypeptide in this way.
  • the isolation and purification of the polypeptide is not a simple matter.
  • a fermentation broth as neutralised, for example by acidification or heating.
  • the bacterial cells are removed to leave a liquid supernatant, containing unwanted soluble by-products, which is discarded.
  • the resultant bacterial cell mass is re-suspended in an appropriate medium, e.g. a suitable buffer and the cells are disrupted to extract and isolate the crude interferon.
  • This laborious procedure is carried out in order to separate the polypeptide of interest from as much fermentation by-products and other contaminants as possible to ensure that subsequent purification steps (involving chromatographic separation) proceed in as an efficient manner as possible.
  • a recombinant polypeptide of interest for example of a recombinant interferon alpha 2
  • a host cell comprising a periplasm like a Gram-negative bacterial cell
  • an osmotic shock on the host cells comprising an expressed recombinant polypeptide of interest in their periplasm, thereby omitting the aforementioned separation and re-suspension steps.
  • the outer cell membrane of the host cell is sufficiently disrupted as to release the contents of its periplasm into the fermentation medium.
  • cytoplasmic material e.g. host-cell proteins and DNA in the cell debris fraction
  • subsequent chromatographic purification is not compromised, but readily leads to superior yields and/or purity of the recombinant polypeptide to be isolated.
  • Suitable recombinant periplasmic expression systems in particular expression vectors, and corresponding prokaryotic host cells as well as appropriate fermentations methods are well known in the art. Suitable examples are described below in the Examples section.
  • said osmotic shock is performed by adding an agent directly to the fermentation medium, wherein said agent is capable of creating after dilution with H 2 O an osmotic pressure leading to disruption of the outer cell membrane of the host cell, and subsequent dilution with H 2 O.
  • the agent is of sucrose.
  • a complex forming component like EDTA, may additionally be added to the fermentation medium.
  • the agent is present in such a concentration as, upon dilution of the fermentation medium with H 2 O, to bring about an osmotic shock which leads to disruption of outer cell membrane of the host cell with subsequent release of the expressed polypeptide of interest.
  • the concentration of the sucrose in the fermentation medium when starting the dilution is about 20% weight/volume.
  • the dilution factor of the sucrose-containing fermentation broth with H 2 O is at least 3 times.
  • a preferred prokaryotic host cell comprising a periplasm is a Gram-negative bacterium.
  • the said Gram-negative bacterium is selected from the group consisting of Escherichia coli, Pseudomonas sp., Enterobacter sp., Campylobacter sp. and Vitreoscilla sp.
  • the host cell is E. coli.
  • the fermentation broth being a crude preparation of the recombinant polypeptide of interest
  • a separation step e.g. high speed centrifugation
  • cellular debris and other particulate matter can be separated from the extract containing the polypeptide of interest.
  • a suitable precipitating agent e.g. polyethyleneimine is a particularly good precipitating agent for this step.
  • the polyethylenelmine is preferably employed at a concentration of about 0.05% and in a medium which is pH adjusted to about 7.5, e.g. 7.3 to 7.7.
  • the process of the present invention can be utilized in the production of a large variety of polypeptides of interest.
  • the polypeptide of interest can be selected from the group consisting of an interferon, an interleukin, a growth hormone, a growth factor, a cytokine, an enzyme, an enzyme inhibitor, an antibody and an antibody fragment, and the like, for example interferon alpha 2A, interferon alpha 2B, interleukin-3, interleukin-6, human growth hormone, insulin, granulocyte-colony stimulating factor, granulocyte macrophage-colony stimulating factor, macrophage-colony stimulating factor, interferon beta 1, bovine somatropin, porcine somatropin, interleukin-11, interleukin-2, a Fab-fragment, and small peptides such as calcitonin, parathyroid hormone (PTH), or a glucagon.
  • PTH parathyroid hormone
  • the polypeptide of interest is a recombinant human interferon 2, in particular human interferon alpha 2A or human interferon alpha 2B, the latter being particularly preferred to be the polypeptide of interest.
  • the extract comprising the polypeptide of interest may contain a number of impurities, for example host-cell proteins and host-cell DNA which have to be removed before the interferon can be formulated into a finished dosage form.
  • the polypeptide is purified by precipitation and chromatographic separation techniques, which are known per se.
  • the polypeptide may be purified using multi-step chromatographic separation.
  • Another aspect of the present invention relates to a process for the preparation of a recombinant interferon alpha 2, comprising
  • the crude preparation of the recombinant interferon alpha 2 is obtained by a process comprising
  • periplasmic expression systems in particular expression vectors, and corresponding prokaryotic host cells as well as appropriate fermentations methods are well known in the art. Suitable examples are described below in the Examples section.
  • said osmotic shock is performed by adding an agent directly to the fermentation medium, wherein said agent is capable of creating after dilution with H 2 O an osmotic pressure leading to disruption of the outer cell membrane of the host cell, and subsequent dilution with H 2 O.
  • the agent is sucrose.
  • a complex forming component like EDTA, may additionally be added to the fermentation medium.
  • the agent is present in such a concentration as, upon dilution of the fermentation medium with H 2 O, to bring about an osmotic shock which leads to disruption of outer cell membrane of the host cell with subsequent release of the expressed polypeptide of interest.
  • the concentration of the sucrose in the fermentation medium when starting the dilution is about 20% weight/volume.
  • the dilution factor for the sucrose-containing fermentation broth with H 2 O is at least 3 times.
  • a preferred prokaryotic host cell is a Gram-negative bacterium, which preferably is selected from the group consisting of Escherichia coli, Pseudomonas sp., Enterobacter sp., Campylobacter sp. and Vitreoscilla sp, E. coli being particularly preferred.
  • Said interferon alpha 2 preferably is selected from the group consisting of interferon alpha 2A and interferon alpha 2B. In a most preferred embodiment, said interferon alpha 2 is interferon alpha 2B.
  • the pH of the crude interferon alpha 2-containing extract obtained from the extraction step may be adjusted to a pH of about 4.8 to 5.5 and may optionally be passed through a filter system (e.g. 0.3 micrometre filter system).
  • the treated extract is thereafter eluted on a CEX column.
  • Any cation-exchange column known in the art may be useful for separating the extracted interferon alpha 2 from impurities.
  • the column is packed with S ceramic Hyper D F.
  • the equilibration eluent is preferably sodium acetate (20mM) + NaCl (70mM) at a pH of 5.0.
  • the interferon is run on the column preferably using a step gradient at 175mM NaCl.
  • the pH of the desired interferon alpha 2-containing fraction eluted from the CEX column may be adjusted to about 7.3. to 7.7 with an appropriate alkaline material, e.g. sodium hydroxide, and the conductivity of the fraction may be adjusted to about 3.5 to 4.5 mS/cm by dilution using purified water.
  • an appropriate alkaline material e.g. sodium hydroxide
  • the fraction is fed onto an anion-exchange column to effect the process of step ii).
  • Any anion exchange column known in the art may be useful for separating the extracted interferon from impurities.
  • the column is packed with Ceramic Q HyperD F resin.
  • the equilibration is preferably 20mM Tris-HCl at pH 7. and thus at high flow rates, e.g. 4 - 8 cm/min.
  • the desired interferon fraction may be eluted after washing the column with equilibration buffer by adding a suitable ionic solute, e.g. sodium chloride at a concentration of up to 1000 mM, preferably 150mM.
  • the temperature at which the separation is run is preferably from 10°C to 15°C.
  • This anion exchange step is highly efficient and the purity of the interferon in the interferon fraction resultant from step ii) may be greater than 40% as determined by reverse-phase high performance liquid chromatography.
  • step iii) in the purification process is a Hydrophobic Interaction Chromatography (HIC) step and is adapted to remove, inter alia substantial amounts of these proteins.
  • the step is carried out on a column packed with a suitable resin for this purpose.
  • the resin is 15PHE (Pharmacia).
  • the interferon fraction to be eluted on the column is first diluted (1:1) with a sodium sulphate solution to a concentration of 0.5M sodium sulphate. Thereafter, the fraction is pH adjusted to about 7.3 to 7.7 with a suitable acid or base, e.g.
  • Step iv) is a further cation exchange chromatography (CEX) step which serves to remove residual DNA and residual host-cell proteins which may have been carried over from previous steps.
  • CEX cation exchange chromatography
  • a CEX column is packed with a suitable packing material, e.g. Toyopearl SP-650 S (TosoHaas).
  • the fraction obtained from step iii) may be diluted with purified water to a final conductivity of about 7.5 to 8.5 mS/cm, adjusted to a pH of 4.3 to 4.7 with, for example with 99-100% acetic acid, and applied to the column.
  • the column is washed and thereafter interferon alpha 2 is eluted during a linear sodium chloride gradient (0-300mM NaCl) at about 250mM NaCl.
  • Eluted fractions having a purity of greater than or equal to 95 area% interferon main peak and no single impurity greater than or equal to 3 area % as measured by IPC reversed-phase HPLC may be collected and processed immediately in the next purification step.
  • Step v) is a size exclusion chromatography step which is employed to remove dimers and any other aggregates and, where applicable, also to perform a buffer change which may be necessary before the interferon product can be formulated into a finished dosage form.
  • any column and packing material suitable for gel filtration may be employed for this final step.
  • the packing material employed is Superdex 75pg.
  • the packing material is chosen for its good resolution capabilities even at relatively high load volumes of, for example about 5 to 15%.
  • the column is equilibrated with an equilibration buffer before being loaded with the interferon fraction from the previous step iv). Thereafter the interferon fraction is eluted off the column using a suitable buffer which preferably consists of 25 mM sodium phosphate, 130 mM sodium chloride and 0.3 mM EDTA at a pH of 7.1 - 7.7 to provide a final bulk solution containing the interferon alpha 2 product.
  • the process as hereinabove described constitutes an efficient process of obtaining an interferon alpha 2 product which is applicable on an industrial scale. It is possible to obtain yields of the interferon product exceeding 100 mg per liter of fermentation broth.
  • interferon alpha 2 polypeptide of the present invention may be formulated into finished dosage forms suitable for administering to humans.
  • Formulations containing interferon alpha 2 products of the present invention may be formulated as injectable formulations.
  • injectable formulations may be provided as lyophilised products that should be reconstituted with water before administration.
  • injectable formulations may be provided as injectable for solutions as single or multidose preparations.
  • injectable formulations may additionally comprise excipients commonly known in the art.
  • Such formulations are useful in the treatment of Hepatitis C.
  • the dosage may depend on the various factors such as the method of administration, age and/or individual condition.
  • Example 1 Construction of a host cell strain for production of recombinant human interferon alpha 2B (rhIFN ⁇ 2B)
  • the polypeptide rhIFN ⁇ 2b (recombinant human Interferon- ⁇ 2b) is produced in the Escherichia coli K-12 strain W3110 transformed with a plasmid containing an optimized synthetic gene coding for rhIFN ⁇ 2b.
  • rhIFN ⁇ 2b is produced under the control of the promoter and Ribosome Binding Site (RBS) of the glutaryl 7-ACA acylase gene ( gac ) from Pseudomonas diminuta CCM 3987 by fermentation of recombinant E. coli K-12.
  • rhIFN ⁇ 2b is expressed as an N-terminal fusion protein with the signal sequence from the same ( gac ) gene, directing the protein to the periplasm with concurrent processing (cleaving off) of the signal sequence.
  • the fermentation process therefore directly yields mature rhIFN ⁇ 2b with a primary sequence identical to that of naturally occurring human Interferon alpha 2b.
  • the expression plasmid is designated pMG414, the production strain W3110[pMG414].
  • pUC19 serves as the starting point for the construction of the vector plasmid.
  • pUC19 is a frequently used and thoroughly characterized high copy plasmid. It contains a highly efficient origin of replication and an ampicillin resistance ( amp or bla ) gene (Yanisch-Perron et al., 1985; Vieira and Messing, 1982; GenBank accession numbers L09137 and X02514). Even though pUC19 is frequently used for the construction of expression plasmids, the amp gene may not be an ideal selectable marker for industrial purposes.
  • the promoter and the coding region of the amp gene are removed and replaced by the promoter and the coding region of the tetracycline resistance gene ( tet ) from the well known safety plasmid pBR322 (Bolivar et al., 1977a, 1977b, 1978; review: Balbás et al., 1986; GenBank accession numbers J01749, K00005, L08654, M10283, M10286, M10356, M10784, M10785, M10786, M33694, V01119).
  • This cloning work is performed with the help of high fidelity PCR techniques.
  • the fragment spanning bps 1743 to 679 of pUC19 is amplified using high fidelity PCR (Pwo DNA Polymerase system from Roche Biochemicals) and the following 5'-phosphorylated oligonucleotides:
  • the resulting PCR fragment is 1624 bps in length and contains the complete pUC19 backbone lacking the amp promoter and coding sequence, but including the stop codon and transcription terminator from the amp gene.
  • the tet promoter and coding sequence (excluding the stop codon) is amplified from pBR322. Again, high fidelity PCR was used to amplify bps 4 to 1273 of pBR322. The following 5'-phosphorylated oligonucleotides were used for this amplification:
  • the resulting PCR fragment is 1270 bps in length.
  • the two PCR fragments are purified by preparative agarose gel electrophoresis and ligated using T4 DNA Ligase (Rapid DNA Ligation Kit, Roche Biochemicals).
  • the ligated DNA is purified and electroporated into Escherichia coli K-12 DH10B (Life Technologies ElectroMAX DH10B electrocompetent cells, genotype: F - mcr A ⁇ ( mrr-hsd RMS- mcr BS) ⁇ 80d lac Z ⁇ M15 ⁇ lac X74 deoR recA1 end A1 ara D139 ⁇ ( ara , leu )7697 gal U ga /K ⁇ - rps L nup G).
  • Transformed cells are plated on to LB agar 15 mg/L tetracycline and 3 g/L glucose. Liquid cultures are grown in LB broth containing 15 mg/L tetracycline and 3 g/L glucose and plasmid DNA is isolated from these cultures using standard miniprep methods. Plasmid DNAs are analyzed by restriction analysis for correct integration of the tet fragment into the pUC19 backbone. Since integration of the fragment was unspecific with respect to orientation, only about 50% of all insert containing clone had the fragment inserted in the correct orientation, i.e. the tet gene running in the same direction as the the amp gene in pUC19. A larger amount of DNA is isolated from liquid cultures of a few clones and subjected to more detailed restriction analyses. Of those clones showing correct restriciton patterns, one is selected for further cloning work.
  • the respective plasmid was designated pMG402. It is identical to pUC19 in all features and functions but for the fact that it must be grown on/in tetracycline-containing media instead of ampicillin-containing media. This way a tet resistant high copy vector suitable for industrial purposes is generated.
  • Sac II restriction endonuclease site is introduced via the 3' PCR primer creating a silent mutation (amino acid sequence unchanged). This Sac II site allows fusion of the gac1ss coding region with the rhIFN ⁇ 2b gene.
  • the structural gene for rhIFN ⁇ 2b is synthesized chemically. It differs from the natural human cDNA sequence in 48 of 165 codons and is designed to eliminate any weak and error prone codons.
  • the resulting gene allows efficient and precise transcription and translation of rhIFN ⁇ 2b in Escherichia coli. Since the gene is designed for expression in a bacterial system it does not contain any untranslated sequences (introns etc.).
  • the structural gene is chemically synthesized.
  • overlapping complementary oligonucleotides about 30 to 50 nucleotides in length are synthesized in a way to cover both strands of the structural gene sequence without any gaps.
  • the oligonucleotides are hybridized to each other and ligated using T4 DNA Ligase.
  • the reaction product is cut with restriction endonucleases and cloned into the pUC18 vector.
  • the resulting plasmid is sequenced and shows the correct sequence.
  • the synthetic gene on this plasmid does not contain the gac signal sequence. This part of the coding region is introduced via the gac fragment containing promoter, RBS and signal sequence and fused to the rhIFN ⁇ 2b structural gene.
  • the gac fragment is generated by chemical synthesis. For example, overlapping complementary oligonucleotides about 30 to 50 nucleotides in length are synthesized in a way to cover the full length of both strands of the gac fragment (including the restriction endonuclease recognition sites on both sides plus a minimum of 6 additional basepairs to allow efficient cleavage) without any gaps.
  • the oligonucleotides are then hybridized to each other (e.g. by heating and subsequent cooling) and ligated using T4 DNA Ligase.
  • the reaction product is then cut with the respective restriction endonucleases ( Xba I and EcoR I) and cloned into the pMG402 vector (see below).
  • the gac fragment containing promoter, RBS and signal sequence can be amplified from a plasmid comprising such elements like plasmid pKS55, which construction is described in CS patent No. 278,515.
  • the gac gene cloned therein has been derived from a strain of Pseudomonas diminuta (CCM 3987). Amplification is carried out using a high fidelity PCR system. The restriction endonuclease sites needed for cloning are introduced via the following PCR primers.
  • the thus created gac fragment has the following nucleotide sequence (SEQ ID NO 8):
  • the gac fragment (either synthetic or created via PCR) and the vector plasmid pMG402 are ligated using the Xba I and EcoR I sites. This way the expression vector pMG412 is generated.
  • the expression vector, pMG412 contains codons 1 - 23 + the first nucleotide of codon 24 of the gac signal sequence. Into codons 22-24 the Sac II site is introduced by silent mutation. Anything downstream of the Sac II site in pMG412 is primer or vector sequence.
  • a suitable primer has the following nucleotide sequence (SEQ ID NO 10):
  • the last amino acids (24-27) of the gac signal sequence are V A F A (SEQ ID NO 11).
  • the rhIFN ⁇ 2b gene is amplified using a high fidelity PCR system.
  • the 5' PCR primer contains the Sac II site for fusing the gene with the gac fragment plus the last four codons of the gac signal sequence.
  • the 3' primer contains the TAA (ochre) stop codon and the Mlu I site for cloning.
  • the amplification of the Interferon alpha structural gene generates the following fragment (SEQ ID NO 12):
  • This rhIFN ⁇ 2b PCR fragment and pMG412 are ligated using the Sac II and Mlu I sites. This way the final production/expression plasmid pMG414 was generated. Both strands of pMG414 are sequenced and show no differences to the expected sequence.
  • plasmid pMG414 (total size 3668 bps): bps 2728-256: pUC19 backbone, part 1 bps 257-546: gac fragment (promoter, RBS, signal sequence) bps 547-1044: synthetic rhIFN ⁇ 2b gene (including TAA stop) bps 1045-1454: cloning sites + pUC19 backbone, part 2 bps 1455-2727: tet gene from pBR322 (promoter/RBS 1455-1536, coding sequence including TAA stop 1537-2727)
  • the gac fragment containing promoter, RBS and signal sequence is fused to the rhIFN ⁇ 2b structural gene - using a restriction endonuclease site at the 3' end of the gac fragment introduced by a PCR primer.
  • the same site is fused to the 5' end of the rhIFN ⁇ 2b structural gene, also by the way of a PCR primer. So after cloning both elements ( gac fragment and rhIFN ⁇ 2b structural gene) into the basic vector a gene encoding a gac1ss-rhIFN ⁇ 2b fusion protein is generated.
  • the first 27 encode the gac signal sequence not present in the final protein and amino acids 28 to 192 encode mature rhIFN ⁇ 2b (165 amino acids, cysteine 1 to glutamic acid 165)
  • nucleotide sequence of the expression cassette used in the rhIFN ⁇ 2b expression plasmid pMG414 (807 bps) (see below) and amino acid sequence of the gac1ss-rhIFN ⁇ 2b fusion protein is shown as follows (SEQ ID NO 13):
  • the start (ATG) and the stop (TAA) codons of the open reading frame are shown in bold.
  • TGC The first (TGC) an the last (GAA) codon of mature rhIFN ⁇ 2b are underlined.
  • restriction endonuclease sites used for cloning are boxed. These are:
  • the gac promoter shows high constitutive / basal activity, the addition of a chemical inducer or a physical stimulus (change in culture conditions) is not required.
  • reaction After electroporation the reaction is suspended in liquid medium and plated onto agar plates containing tetracycline.
  • the best clone may show good productivity but relatively poor growth. This poor growth can result from various factors, e.g. product toxicity to the host cell, metabolic burden due to product synthesis etc.
  • the addition of glucose often brings some improvement because glucose downregulates (e.g. by catabolite repression) many promoters used for recombinant protein expression.
  • glucose has a general positive effect on the growth of E. coli because it can be directly introduced into the metabolism as a carbon source.
  • a cryovial of E1/116 is thawed and the cell suspension streaked onto glucose free LB agar plates containing tetracycline.
  • the plate is incubated at 37°C until the colonies reach a sufficient size for inoculating a liquid culture. Colonies are transferred from the plate into small shake flasks filled with 15 mL of glucose free LB broth containing tetracycline.
  • the cultures are shaken at 37°C until they reach an optical density at 600 nm of above 0.5 (typically > 1.0). For this first round this takes up to 48 hours due to the poor growth characteristics of the original isolate.
  • This PSL is used as a starting point for the generation of the GMP cell banks (Master Cell Bank and Working Cell Bank) of the Interferon alpha 2b production strain.
  • This reisolate is designated E1/116a. Reisolation processes like the one described above have proved to yield reproducible results.
  • E1/116a shows excellent growth characteristics in shake flasks and stirred bioreactors (fermenters).
  • An inoculum suitable for starting a bioreactor can be grown in a shake flask starting from a Working Cell Bank vial in about 8 hours.
  • a Master Cell Bank is prepared under cGMP conditions from the primary seed lot described above.
  • a PSL vial is thawed and plated onto tetracycline containing agar plates.
  • a single colony is picked and used to inoculate the Master Cell Bank (MCB) shake flask culture (LB broth medium containing tetracycline).
  • MMB Master Cell Bank
  • the cell supension from the logarithmic growth phase is mixed 1+1 with 40 % w/v Glycerol, aliquoted at 1.8 mL into cryogenic vials, sealed in cryogenic tubing, and frozen in the liquid phase of a liquid nitrogen tank.
  • the Working Cell Bank is generated in the same way as the Master Cell Bank except that the shake flask culture is inoculated with cell suspension from a thawed MCB vial.
  • Example 2 Fermentation process for production of recombinant human interferon a 2B (rhIFN ⁇ 2B)
  • the fermentation process is started by growing the strain E.coli K-12 W3110 obtainable from the Working Cell Bank as described above in shake flask cultures in Luria Bertani (LB-) medium at 37°C with the addition of the antibiotic tetracyclin hydrochloride to avoid growth of non-plasmid carrying cells.
  • the medium for this pre-culture cultivation is based on deionized water containing glucose as a sole carbon source and yeast autolysate as a complex nitrogen source.
  • anorganic salts like KH 2 PO 4 , K 2 HPO 4 , (NH 4 ) 2 SO 4 and MgSO 4 .7H 2 O are added to the medium.
  • polypropylene glycole 2000 (PPG2000) is used as an antifoam agent polypropylene glycole 2000 (PPG2000) is used.
  • the pre-culture medium has the following composition:
  • Component Amount De-ionized water (WBI) 30 l Yeast autolysate, KAT, Ohly 21.7 g/l Glucose Monohydrate, pure 25.0 g/l Ammonium Sulfate, p.a. 1.0 g/l Potassium Phosphate Monobasic, p.a 1.5 g/l Potassium Phosphate Dibasic, anhydrous, pure 3.0 g/l Magnesium Sulfate Heptahydrate, p.a. 0.5 g/l Polypropylene Glycole 2000 0.5 ml/l
  • the cultivation-time for seed culture is about 16 hours.
  • pH-value is controlled to a set-point of 7,0 ⁇ 0,2 with sulfuric acid and sodium hydroxide or concentrated ammonia solution.
  • Concentration of dissolved oxygen is kept at levels higher than 20% of saturation by increasing the stirrer speed.
  • Stirrer speed at the beginning of the cultivation is set to 300 rpm, back-pressure in the vessel to 0,3 bar and aeration rate is controlled to 30 Umin (equivalent to "1 vvm").
  • Temperature is kept constantly at 37°C during cultivation. As a transfer criterion of broth to the main stage of the fermentation process, an increase of the dissolved oxygen concentration after consumption of the carbon source is used.
  • a medium based on deionized water glucose as a carbon source and yeast autolysate as a complex nitrogen source is used.
  • anorganic salts NH 4 ) 2 SO 4 , CaCl 2 .2H 2 O and MgSO 4 .7H 2 O
  • PPG 2000 is used as an antifoam agent.
  • the initial glucose is sterilized separatly and added to the sterile rest of the medium.
  • Inoculum size to the main fermenter medium was in a range between 0,75 and 3%.
  • the main culture medium has the following composition:
  • Component Amount Deionized water (WBI) 60 l Yeast autolysate, KAT, Ohly 43.5 g/l Ammonium Sulfate, p.a. 1.0 g/l Calcium Chloride Dihydrate cryst., p.a. 0.3 g/l Magnesium Sulfate Heptahydrate, p.a. 1.0 g/l Polypropylene Glycole 2000 0.5 ml/l
  • the most important point during this cultivation is the necessity of a complete consumption of the initial glucose present in the medium. This leads to a sharp increase of dissolved oxygen concentration after about 9 hours of growth.
  • Glucose limitation controlled by the feeding of the glucose-solution at a constant rate is therefore very important.
  • the temperature during cultivation is controlled to a constant value of about 28°C.
  • the initial stirrer speed is set to 300 rpm, the aeration rate is controlled to 100 Umin (equivalent to "1 vvm") and the back-pressure in the vessel is set to 0,3 bar.
  • the pH-value is controlled to 7,1 ⁇ 0,3 with sulfuric acid and sodium hydroxide or concentrated ammonia solution. A peak of the pH-value up to 8.0 after consumption of the initially supplied glucose is acceptable.
  • the concentration of the dissolved oxygen is controlled to values higher than 20% of saturation.
  • Dependent on the oxygen transfer capacity of the bioreactor DO-concentration is kept at levels higher than 20% of saturation, preferably between about 40 % and 100% of saturation, by first increasing the stirrer speed to a maximum value. If this is not sufficient, first aeration rate and after that back-pressure is increased, respectively.
  • the culture is harvested and cooled to 15 ⁇ 5 °C and conditioned for downstream processing by the addition of sucrose/EDTA to the cooled broth.
  • the results of a fermentation batch is analysed based on the Westernblot technique or on HPLC-measurements after laboratory or pilot plant periplasmatic extraction of the product.
  • a fermentation broth containing host cells comprising the expressed interferon alpha 2B in the periplasmic space is adjusted with sulfuric acid to pH of 5,0 ⁇ 0,1 immediately after the fermentation and cooled down to 4°C ⁇ 2 °C.
  • the low pH and the low temperature help to inactivate endogenous proteases.
  • the fermentation broth is adjusted to 10°C to 20°C, then without any concentration or washing of the cells, solid or liquid sucrose (200g sucrose/kg fermentation broth) and EDTA (concentration 10mM) are added and the pH adjusted to 8.0.
  • solid or liquid sucrose 200g sucrose/kg fermentation broth
  • EDTA concentration 10mM
  • the pH adjusted to 8.0 After a selective one-step cell permeation protocol using osmotic shock (1+3 dilutions) with cooled water, whereby the fermentation broth comprising sucrose and EDTA is poured or pumped into the cooled (temperature about 4°C) water, the released periplasmic extract is clarified.
  • Polyethyleneimine is added to a final concentration of 0,05 % and the pH is adjusted to about 7,5 with acetic acid. After 15 to 45 minutes cell debris and DNA flocculate, leaving a clear crude extract containing interferon which may be subject to centrifugation to improve clarity.
  • Example 3 After pH adjustment to 4.8 - 5.2 with acetic acid and a filtration step using a 0.3 micron filter, the crude extract of Example 3 is applied to the CEX column (S ceramic HyperD F (Biosepra)). After a washing step with an equilibration buffer (20mM sodium acetate and 70mM NaCl at pH 5.0) the interferon is eluted with a step gradient at 175mM NaCl. The fraction collected is immediately processed by the process step of Example 4.2.
  • an equilibration buffer (20mM sodium acetate and 70mM NaCl at pH 5.0
  • Example 4.1 The fraction from Example 4.1 is adjusted to a pH of 7.3 to 7.7 with sodium hydroxide, diluted and purified with water to a conductivity of 3.5 to 4.5 mS/cm and applied to the AEX column (Q ceramic HyperD F (Biosepra)). After washing, the interferon is eluted with a linear salt gradient (0-300mM NaCl) at about 150mM NaCl. Fractions are collected that have a purity of greater than or equal to 90 area % according to IPC reversed-phase HPLC and used directly in the next step (see Example 4.3).
  • Example 4.2 The fraction of Example 4.2 is diluted (1:1) with a stock solution of sodium sulphate (0.5% sodium sulphate), adjusted to pH 7.3 to 7.7 with NaOH or HCl and applied to the HIC column (Source 15PHE (Pharmacia). After washing, the interferon fraction of Example 3 is eluted with a linear sodium sulphate concentration (800 - 0 mM sodium sulphate) at about 400mM sodium sulphate. The fractions collected that have a purity of greater than or equal to 93 area % and no impurity greater than or equal to 3% according to IPC reversed-phase HPLC are used directly in the next purification step.
  • Example 4 The collected fractions of Example 4 are diluted with water to a final conductivity of 7.5 to 8.5 mS/cm, adjusted to pH 4.3 to 4.7 with 99 to 100% acetic acid and applied to the CEX column (Toyopearl SP-650 S (TosoHaas)). After a washing step, the interferon is eluted in a linear NaCl gradient (0 - 300 mM NaCl) at about 250mM NaCl. The fractions are collected that have a purity of greater than or equal to 95 area % and no impurity greater than or equal to 3% according to IPC reversed-phase HPLC and are used directly in the next purification step.
  • the last purification step is a gel filtration step to remove dimers and other aggregates and to perform a buffer exchange for the final formulation.
  • the Superdex 75 pg used in this step shows a good resolution even at a high load volume (5 % - 15 %).
  • the SEC is performed in 25mM sodium phosphate and 130mM NaCl + 0.3mM EDTA at a pH of about 7.3 to 7.7.
  • E. coli strain W3110 (ATCC 27325), as used herein, has been deposited with the American Type Culture Collection (ATCC), 10801 University Boulevard, Manassas, VA 20110-2209, USA on February 28, 2001, under the Designation No. PTA-3132.

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Claims (9)

  1. Procédé de préparation d'un polypeptide recombinant d'intérêt, comprenant
    (i) la fermentation d'une cellule hôte procaryote comprenant un périplasme et étant transformée avec un système d'expression recombinant capable de réaliser la sécrétion d'un polypeptide d'intérêt dans le périplasme de ladite cellule hôte, où ladite fermentation est réalisée dans un milieu de fermentation dans des conditions telles que le polypeptide d'intérêt est sécrété dans le périplasme de la cellule hôte, et
    (ii) l'extraction du polypeptide d'intérêt à partir du périplasme en appliquant un choc osmotique aux cellules hôtes contenues dans le milieu de fermentation,
    où ledit choc osmotique est réalisé en ajoutant du saccharose directement au milieu de fermentation et ensuite en diluant avec H2O de telle manière que la membrane cellulaire externe de la cellule hôte est suffisamment rompue pour libérer le contenu de son périplasme dans le milieu de fermentation.
  2. Procédé selon la revendication 1, dans lequel la concentration du saccharose dans le milieu de fermentation au départ de la dilution est d'environ 20 % en poids/volume.
  3. Procédé selon la revendication 2, dans lequel le facteur de dilution du bouillon de fermentation contenant le saccharose avec H2O est d'au moins 3 fois.
  4. Procédé selon la revendication 1, dans lequel ladite cellule hôte procaryote est une bactérie Gram négatif.
  5. Procédé selon la revendication 4, dans lequel ladite bactérie Gram négatif est choisie dans le groupe constitué par Escherichia coli, Pseudomonas sp, Enterobacter sp, Campylobacter sp et Vitreoscilla sp.
  6. Procédé selon la revendication 5, dans lequel la bactérie Gram négatif est E. coli.
  7. Procédé selon la revendication 1, dans lequel le polypeptide d'intérêt est choisi dans le groupe constitué par un interféron, une interleukine, une hormone de croissance, un facteur de croissance, une cytokine, une enzyme, un inhibiteur enzymatique, un anticorps et un fragment d'anticorps.
  8. Procédé selon la revendication 1, dans lequel le polypeptide d'intérêt est un interféron alpha 2.
  9. Procédé selon la revendication 8, dans lequel l'interféron alpha 2 est choisi dans le groupe constitué par l'interféron alpha 2A et l'interféron alpha 2B.
EP04764055A 2003-08-13 2004-08-12 Procédé de purification des polypeptides recombinants Expired - Lifetime EP1656455B1 (fr)

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PL2102354T3 (pl) 2007-01-12 2018-01-31 Dow Global Technologies Llc Urządzenie i sposoby osmotycznego szokowania komórek
KR20100103595A (ko) * 2008-01-18 2010-09-27 에프. 호프만-라 로슈 아게 비-글라이코실화된 단백질의 정제
WO2012022688A1 (fr) * 2010-08-20 2012-02-23 Boehringer Ingelheim International Gmbh Procédé d'inactivation de protéases dans un liquide obtenu d'une culture cellulaire par modification du ph
AU2013224027B2 (en) 2012-02-23 2019-01-24 Juno Therapeutics Gmbh Chromatographic isolation of cells and other complex biological materials
RU2644652C2 (ru) * 2012-09-17 2018-02-13 Ф.Хоффманн-Ля Рош Аг Способ получения полипептидов в периплазме прокариотических клеток
MA45489A (fr) 2015-10-22 2018-08-29 Juno Therapeutics Gmbh Procédés de culture de cellules, kits et appareil associés
RU2021134624A (ru) 2015-10-22 2022-03-15 Джуно Терапьютикс Гмбх Способы, наборы, средства и устройства для трансдукции
JP7339160B2 (ja) 2017-04-27 2023-09-05 ジュノ セラピューティクス ゲーエムベーハー オリゴマー粒子試薬およびその使用方法
CN113249391A (zh) * 2021-05-10 2021-08-13 江苏坤力生物制药有限责任公司 一种编码rPD蛋白的核酸、其制备方法和用途

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WO2005017174A2 (fr) 2005-02-24
WO2005017174A3 (fr) 2005-08-18
SI1656455T1 (sl) 2012-12-31
ES2391457T3 (es) 2012-11-26
JP2007501622A (ja) 2007-02-01
US20060173167A1 (en) 2006-08-03

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